JPS6247058B2 - - Google Patents
Info
- Publication number
- JPS6247058B2 JPS6247058B2 JP55021709A JP2170980A JPS6247058B2 JP S6247058 B2 JPS6247058 B2 JP S6247058B2 JP 55021709 A JP55021709 A JP 55021709A JP 2170980 A JP2170980 A JP 2170980A JP S6247058 B2 JPS6247058 B2 JP S6247058B2
- Authority
- JP
- Japan
- Prior art keywords
- absorption liquid
- absorption
- chloride
- trichloride
- gas
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Expired
Links
- 238000010521 absorption reaction Methods 0.000 claims description 64
- 239000007788 liquid Substances 0.000 claims description 40
- ZMXDDKWLCZADIW-UHFFFAOYSA-N N,N-Dimethylformamide Chemical compound CN(C)C=O ZMXDDKWLCZADIW-UHFFFAOYSA-N 0.000 claims description 12
- 229910021591 Copper(I) chloride Inorganic materials 0.000 claims description 10
- OXBLHERUFWYNTN-UHFFFAOYSA-M copper(I) chloride Chemical compound [Cu]Cl OXBLHERUFWYNTN-UHFFFAOYSA-M 0.000 claims description 10
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims description 7
- 229910002091 carbon monoxide Inorganic materials 0.000 claims description 7
- SECXISVLQFMRJM-UHFFFAOYSA-N N-Methylpyrrolidone Chemical compound CN1CCCC1=O SECXISVLQFMRJM-UHFFFAOYSA-N 0.000 claims description 5
- 150000001408 amides Chemical class 0.000 claims description 5
- 229940045803 cuprous chloride Drugs 0.000 claims description 5
- 229910021381 transition metal chloride Inorganic materials 0.000 claims description 5
- 239000002904 solvent Substances 0.000 claims description 4
- JIAARYAFYJHUJI-UHFFFAOYSA-L zinc dichloride Chemical compound [Cl-].[Cl-].[Zn+2] JIAARYAFYJHUJI-UHFFFAOYSA-L 0.000 claims description 4
- RYGMFSIKBFXOCR-UHFFFAOYSA-N Copper Chemical compound [Cu] RYGMFSIKBFXOCR-UHFFFAOYSA-N 0.000 claims description 3
- 229910052802 copper Inorganic materials 0.000 claims description 3
- 239000010949 copper Substances 0.000 claims description 3
- RBTARNINKXHZNM-UHFFFAOYSA-K iron trichloride Chemical compound Cl[Fe](Cl)Cl RBTARNINKXHZNM-UHFFFAOYSA-K 0.000 claims description 3
- AVQQQNCBBIEMEU-UHFFFAOYSA-N 1,1,3,3-tetramethylurea Chemical compound CN(C)C(=O)N(C)C AVQQQNCBBIEMEU-UHFFFAOYSA-N 0.000 claims description 2
- 229910021556 Chromium(III) chloride Inorganic materials 0.000 claims description 2
- 229910021577 Iron(II) chloride Inorganic materials 0.000 claims description 2
- 229910021380 Manganese Chloride Inorganic materials 0.000 claims description 2
- GLFNIEUTAYBVOC-UHFFFAOYSA-L Manganese chloride Chemical compound Cl[Mn]Cl GLFNIEUTAYBVOC-UHFFFAOYSA-L 0.000 claims description 2
- FXHOOIRPVKKKFG-UHFFFAOYSA-N N,N-Dimethylacetamide Chemical compound CN(C)C(C)=O FXHOOIRPVKKKFG-UHFFFAOYSA-N 0.000 claims description 2
- SUAKHGWARZSWIH-UHFFFAOYSA-N N,N‐diethylformamide Chemical compound CCN(CC)C=O SUAKHGWARZSWIH-UHFFFAOYSA-N 0.000 claims description 2
- 229910021551 Vanadium(III) chloride Inorganic materials 0.000 claims description 2
- 229960000359 chromic chloride Drugs 0.000 claims description 2
- QSWDMMVNRMROPK-UHFFFAOYSA-K chromium(3+) trichloride Chemical compound [Cl-].[Cl-].[Cl-].[Cr+3] QSWDMMVNRMROPK-UHFFFAOYSA-K 0.000 claims description 2
- ORTQZVOHEJQUHG-UHFFFAOYSA-L copper(II) chloride Chemical compound Cl[Cu]Cl ORTQZVOHEJQUHG-UHFFFAOYSA-L 0.000 claims description 2
- 229960003280 cupric chloride Drugs 0.000 claims description 2
- 229960002089 ferrous chloride Drugs 0.000 claims description 2
- NMCUIPGRVMDVDB-UHFFFAOYSA-L iron dichloride Chemical compound Cl[Fe]Cl NMCUIPGRVMDVDB-UHFFFAOYSA-L 0.000 claims description 2
- ICAKDTKJOYSXGC-UHFFFAOYSA-K lanthanum(iii) chloride Chemical compound Cl[La](Cl)Cl ICAKDTKJOYSXGC-UHFFFAOYSA-K 0.000 claims description 2
- 235000002867 manganese chloride Nutrition 0.000 claims description 2
- 239000011565 manganese chloride Substances 0.000 claims description 2
- YBCAZPLXEGKKFM-UHFFFAOYSA-K ruthenium(iii) chloride Chemical compound [Cl-].[Cl-].[Cl-].[Ru+3] YBCAZPLXEGKKFM-UHFFFAOYSA-K 0.000 claims description 2
- YONPGGFAJWQGJC-UHFFFAOYSA-K titanium(iii) chloride Chemical group Cl[Ti](Cl)Cl YONPGGFAJWQGJC-UHFFFAOYSA-K 0.000 claims description 2
- HQYCOEXWFMFWLR-UHFFFAOYSA-K vanadium(iii) chloride Chemical compound [Cl-].[Cl-].[Cl-].[V+3] HQYCOEXWFMFWLR-UHFFFAOYSA-K 0.000 claims description 2
- 235000005074 zinc chloride Nutrition 0.000 claims description 2
- 239000011592 zinc chloride Substances 0.000 claims description 2
- 150000001875 compounds Chemical class 0.000 claims 2
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims 1
- 229910052799 carbon Inorganic materials 0.000 claims 1
- 239000007789 gas Substances 0.000 description 22
- 238000000926 separation method Methods 0.000 description 10
- 238000000034 method Methods 0.000 description 9
- 239000000243 solution Substances 0.000 description 9
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 8
- 239000007864 aqueous solution Substances 0.000 description 5
- 239000000203 mixture Substances 0.000 description 5
- VEXZGXHMUGYJMC-UHFFFAOYSA-N Hydrochloric acid Chemical compound Cl VEXZGXHMUGYJMC-UHFFFAOYSA-N 0.000 description 4
- 239000012456 homogeneous solution Substances 0.000 description 4
- UHOVQNZJYSORNB-UHFFFAOYSA-N Benzene Chemical compound C1=CC=CC=C1 UHOVQNZJYSORNB-UHFFFAOYSA-N 0.000 description 3
- YXFVVABEGXRONW-UHFFFAOYSA-N Toluene Chemical compound CC1=CC=CC=C1 YXFVVABEGXRONW-UHFFFAOYSA-N 0.000 description 3
- 238000001816 cooling Methods 0.000 description 3
- 239000011521 glass Substances 0.000 description 3
- 230000007062 hydrolysis Effects 0.000 description 3
- 238000006460 hydrolysis reaction Methods 0.000 description 3
- 239000002994 raw material Substances 0.000 description 3
- 150000003839 salts Chemical class 0.000 description 3
- 229910021626 Tin(II) chloride Inorganic materials 0.000 description 2
- 230000002745 absorbent Effects 0.000 description 2
- 239000002250 absorbent Substances 0.000 description 2
- VSCWAEJMTAWNJL-UHFFFAOYSA-K aluminium trichloride Chemical compound Cl[Al](Cl)Cl VSCWAEJMTAWNJL-UHFFFAOYSA-K 0.000 description 2
- 239000000463 material Substances 0.000 description 2
- 235000011150 stannous chloride Nutrition 0.000 description 2
- 238000003786 synthesis reaction Methods 0.000 description 2
- AXZWODMDQAVCJE-UHFFFAOYSA-L tin(II) chloride (anhydrous) Chemical compound [Cl-].[Cl-].[Sn+2] AXZWODMDQAVCJE-UHFFFAOYSA-L 0.000 description 2
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 1
- 229910021578 Iron(III) chloride Inorganic materials 0.000 description 1
- 229910000831 Steel Inorganic materials 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 238000009835 boiling Methods 0.000 description 1
- 125000001309 chloro group Chemical group Cl* 0.000 description 1
- 239000000470 constituent Substances 0.000 description 1
- 238000010276 construction Methods 0.000 description 1
- 239000006185 dispersion Substances 0.000 description 1
- 239000000446 fuel Substances 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 238000002844 melting Methods 0.000 description 1
- 230000008018 melting Effects 0.000 description 1
- 238000011084 recovery Methods 0.000 description 1
- 239000002002 slurry Substances 0.000 description 1
- 239000010959 steel Substances 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 239000004094 surface-active agent Substances 0.000 description 1
Classifications
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02A—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
- Y02A50/00—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE in human health protection, e.g. against extreme weather
- Y02A50/20—Air quality improvement or preservation, e.g. vehicle emission control or emission reduction by using catalytic converters
Landscapes
- Gas Separation By Absorption (AREA)
- Treating Waste Gases (AREA)
Description
【発明の詳細な説明】
本発明は、一酸化炭素（以下、COと記す）の
吸収液に関し、さらに詳しくはCOを含有する各
種ガス源からCOを分離、濃縮して回収するため
の吸収液に関する。[Detailed Description of the Invention] The present invention relates to an absorption liquid for carbon monoxide (hereinafter referred to as CO), and more specifically, an absorption liquid for separating, concentrating, and recovering CO from various gas sources containing CO. Regarding.
化学工業や製鉄工業等において、合成用原料ガ
スの製造または省エネルギといつた考えのもと
に、例えばプロセス排ガスからCOを分離、濃縮
して回収することが大きな技術的課題となつてい
る。 In the chemical industry, steel industry, etc., separating, concentrating, and recovering CO from process exhaust gas has become a major technical issue, with the aim of producing raw material gas for synthesis or saving energy.
COを含有するガス源からCOを分離、濃縮する
方法には、現在、第１銅塩の溶液等の吸収液を使
用する吸収液法、およびこれとは原理的に異る深
冷分離法が知られている。後者の深冷分離法は、
複雑な冷却、熱回収システムから構成されてお
り、操作温度が低温であるため、装置材料として
高価なものを使用する必要があり、また低温を得
るために、動力消費量が大きくなるという欠点が
ある。 Currently, methods for separating and concentrating CO from a gas source containing CO include the absorption liquid method, which uses an absorption liquid such as a solution of cuprous salt, and the cryogenic separation method, which is fundamentally different from this method. Are known. The latter cryogenic separation method is
It consists of a complex cooling and heat recovery system, and because the operating temperature is low, it is necessary to use expensive equipment materials, and it also has the disadvantage of increasing power consumption to obtain the low temperature. be.
一方、吸収液法に使用されるCO吸収液として
は、従来、アンモニア性第１銅塩水溶液または塩
酸性第１銅塩水溶液が用いられてきたが、いずれ
も、水溶液単位体積あたりのCO吸収量が小さい
という問題があつた。これらの吸収液において
は、CO吸収に直接関与する一価の銅を溶液中に
可溶化させるために、クロロ錯体あるいはアンミ
ン錯体を形成させているものと考えられる。また
最近、塩化第１銅（以下、CuClと記す）と無水
塩化アルミニウム（以下、AlCl3と記す）の錯体
（CuAlCl4）をトルエンに溶解させたCO吸収液が
開発され、注目をあつめている。この吸収液は溶
液単位体積あたりのCO吸収量が水溶液系のもの
に較べて非常に高いという特徴を有する。このた
め実際のCO分離、濃縮プロセスに適用する場
合、吸収塔における操作で高圧、低温を必要とせ
ず、常温、常圧で運転が可能なため、装置に耐圧
材料等を必要としないこと、およびCOの吸収負
荷が大きいため、溶液循環量が小さくて済むなど
の利点を有している。 On the other hand, as the CO absorption liquid used in the absorption liquid method, an ammoniacal cuprous salt aqueous solution or a hydrochloric acid cuprous salt aqueous solution has conventionally been used, but in either case, the amount of CO absorbed per unit volume of the aqueous solution is There was a problem that the size was small. In these absorption solutions, it is thought that a chloro complex or an ammine complex is formed in order to solubilize monovalent copper, which is directly involved in CO absorption, in the solution. Recently, a CO absorbent solution in which a complex (CuAlCl 4 ) of cuprous chloride (hereinafter referred to as CuCl) and anhydrous aluminum chloride (hereinafter referred to as AlCl 3 ) is dissolved in toluene has been developed and is attracting attention. . This absorption liquid has a characteristic that the amount of CO absorbed per unit volume of solution is much higher than that of an aqueous solution. Therefore, when applied to actual CO separation and concentration processes, the absorption tower does not require high pressure or low temperature, and can be operated at room temperature and pressure, so the equipment does not require pressure-resistant materials, etc. Since the CO absorption load is large, it has the advantage of requiring only a small amount of solution circulation.
しかし、上記のような吸収液はその構成成分で
あるAlCl3が水または水蒸気と接触して定量的に
加水分解を受け、それに伴いCO吸収量も低下す
るという問題がある。 However, the above absorption liquid has a problem in that its constituent AlCl 3 comes into contact with water or water vapor and undergoes quantitative hydrolysis, resulting in a corresponding decrease in the amount of CO absorbed.
本発明の目的は、水または水蒸気と接触しても
加水分解を受けにくく、高い一酸化炭素吸収性能
を維持する吸収液を提供することにある。 An object of the present invention is to provide an absorption liquid that is resistant to hydrolysis even when it comes into contact with water or steam and maintains high carbon monoxide absorption performance.
上記目的を達成するために、本発明の吸収液
は、塩化第１銅と非プロトン性のアミド系溶液と
を含むことを特徴とする。 In order to achieve the above object, the absorption liquid of the present invention is characterized by containing cuprous chloride and an aprotic amide solution.
上記非プロトン性のアミド系溶媒としては、融
点が20℃以下、沸点が100℃以上のものを対象と
し、Ｎ−メチルピロリドン、テトラメチルウレ
ア、ジメチルホルムアミド、ジエチルホルムアミ
ドまたはジメチルアセトアミドが適当で、特にＮ
−メチルピロリドンおよびジメチルホルムアミド
が好適である。 The above-mentioned aprotic amide solvent has a melting point of 20°C or lower and a boiling point of 100°C or higher, and N-methylpyrrolidone, tetramethylurea, dimethylformamide, diethylformamide or dimethylacetamide are suitable, particularly N
-Methylpyrrolidone and dimethylformamide are preferred.
本発明の吸収液はスラリ、均一溶液のいずれの
状態でも使用可能であるが、操作の容易性という
観点からは均一溶液の方が好ましい。吸収液中の
塩化第１銅等の分散性を改善するために、本発明
においては一価の銅以外の遷移金属塩化物を添加
することが望ましい。このような遷移金属塩化物
としては、加水分解定数の小さい、三塩化チタ
ン、三塩化バナジウム、三塩化クロム、二塩化マ
ンガン、二塩化鉄、三塩化鉄、二塩化銅、二塩化
スズ、塩化亜鉛、塩化ルテニウム又は塩化ランタ
ンが適当で、特に塩化第２鉄および二塩化スズが
好ましい。 The absorption liquid of the present invention can be used in either the form of a slurry or a homogeneous solution, but a homogeneous solution is preferable from the viewpoint of ease of operation. In order to improve the dispersibility of cuprous chloride and the like in the absorption liquid, it is desirable in the present invention to add a transition metal chloride other than monovalent copper. Such transition metal chlorides include titanium trichloride, vanadium trichloride, chromium trichloride, manganese dichloride, iron dichloride, iron trichloride, copper dichloride, tin dichloride, and zinc chloride, which have small hydrolysis constants. , ruthenium chloride or lanthanum chloride are suitable, with ferric chloride and tin dichloride being particularly preferred.
上記各成分の構成比は、塩化第１銅：遷移金属
塩化物：非プロトン性のアミド系溶媒のモル比
で、１：０〜２：４〜60の範囲が適当であり、特
に１：０〜１：６〜30の範囲が好ましい。 The composition ratio of each of the above components is the molar ratio of cuprous chloride: transition metal chloride: aprotic amide solvent, and is suitably in the range of 1:0 to 2:4 to 60, particularly 1:0. -1: The range of 6-30 is preferable.
本発明において、吸収液中の各成分の分散性を
向上させるために適当な界面活性剤などを添加す
ることができる。本発明の構成成分の選択に当つ
ては、吸収液の粘度が小さく、安定性がよいこ
と、また構成成分がCO含有ガスと接触する際、
またはCOを分離する際に系外に揮散しないもの
であることが好ましい。 In the present invention, a suitable surfactant or the like may be added to improve the dispersibility of each component in the absorption liquid. When selecting the components of the present invention, it is important that the absorption liquid has low viscosity and good stability, and that when the components come into contact with CO-containing gas,
Alternatively, it is preferable that it not volatilize out of the system when CO is separated.
次に、本発明の吸収液を使用してCO含有ガス
中のCOを吸収分離し、濃縮COとして回収する際
の操作条件について説明する。 Next, operating conditions for absorbing and separating CO in a CO-containing gas using the absorption liquid of the present invention and recovering it as concentrated CO will be described.
第１図は、本発明の吸収液を用いたCOの分
離、濃縮プロセスの原理的なフローシートであ
る。図において、CO含有ガスは、必要に応じて
前処理装置１で前処理され、原料ガスライン１１
を通じ、吸収塔２に入り、吸収塔内の吸収液と接
触し、COが選択的に吸収される。吸収塔排ガス
は、飛沫同伴成分を適宜除去されたのち、排ガス
ライン２１を通じ大気中に放出される。一方、
COを吸収した液は、吸収ライン３１から熱交換
器４をへて分離塔３に送られ、ここで昇温または
減圧されることより、COを放散する。分離塔か
らの排ガスは高濃度のCOを含有するが、飛沫同
伴成分を除去した後、ガスライン４１をへて回収
され、製品ガスとなる。COを分解した吸収液
は、ライン５１から吸収塔２にもどり循環使用さ
れる。 FIG. 1 is a basic flow sheet of the CO separation and concentration process using the absorption liquid of the present invention. In the figure, CO-containing gas is pretreated in a pretreatment device 1 as necessary, and a raw material gas line 11
, enters the absorption tower 2, contacts the absorption liquid in the absorption tower, and CO is selectively absorbed. The absorption tower exhaust gas is discharged into the atmosphere through the exhaust gas line 21 after the entrained components are appropriately removed. on the other hand,
The liquid that has absorbed CO is sent from the absorption line 31 through the heat exchanger 4 to the separation column 3, where it is heated or depressurized to release CO. The exhaust gas from the separation tower contains a high concentration of CO, but after removing entrained components, it is recovered through the gas line 41 and becomes a product gas. The absorption liquid that has decomposed CO is returned to the absorption tower 2 through the line 51 and is used for circulation.
本発明の吸収液を、実際のCO濃縮、分離プロ
セスに適用する場合の操作温度および圧力は、
CO含有ガス中のCO含有割合、接触時間、吸収液
の組成等に応じて変化することができる。一般に
吸収温度を低下させるとCO吸収量は増加するが
低温生成のための冷却装置が必要となり、また吸
収液の粘度が増加し、時には吸収液が凝固するこ
とがある。一方、吸収温度を余り高くするとCO
吸収量が小さくなる。上記の点から吸収温度は一
般に10〜80℃とすることが好ましい。さらに吸収
圧力は高い方がCO吸収量が大きくなり、また吸
収速度も高くなるが、ガスの圧縮機が必要にな
り、さらに装置を耐圧構造にせねばならず、建設
費が高くなる。このような点から、吸収圧力は一
般にゲージ圧で０〜20Kg／cm2とすることが好まし
い。 The operating temperature and pressure when applying the absorption liquid of the present invention to the actual CO concentration and separation process are as follows:
It can be changed depending on the CO content rate in the CO-containing gas, the contact time, the composition of the absorption liquid, etc. In general, lowering the absorption temperature increases the amount of CO absorbed, but requires a cooling device for low-temperature production, increases the viscosity of the absorption liquid, and sometimes causes the absorption liquid to solidify. On the other hand, if the absorption temperature is too high, CO
Absorption amount becomes smaller. In view of the above, the absorption temperature is generally preferably 10 to 80°C. Furthermore, the higher the absorption pressure, the greater the amount of CO absorbed and the faster the absorption rate, but a gas compressor is required, and the equipment must also have a pressure-resistant structure, which increases construction costs. From this point of view, the absorption pressure is generally preferably 0 to 20 kg/cm 2 in gauge pressure.
COを吸収した吸収液は、吸収温度よりも温度
を下げ、もしくは圧力を下げることにより、また
は不活性の媒体（例えば水蒸気、ベンゼン蒸気等
と接触させることにより、さらにはCOの用途に
よつては水素ガス等と接触させることにより、
COを放散し、再生される。上記放散の操作は単
独でも組合せて行つてもよい。放散されたCOを
捕集すれば濃縮COガスを得ることができるが、
これらのガスは燃料または化学合成用原料ガスと
して有効に利用される。 The absorption liquid that has absorbed CO can be prepared by lowering the temperature or pressure below the absorption temperature, or by contacting it with an inert medium (e.g. water vapor, benzene vapor, etc.), or depending on the use of CO. By contacting with hydrogen gas etc.
Dissipates CO and is regenerated. The above-mentioned dispersion operations may be performed alone or in combination. Concentrated CO gas can be obtained by collecting the emitted CO, but
These gases are effectively used as fuel or raw material gas for chemical synthesis.
以下、本発明を実施例により更に詳細に説明す
る。なお、実施例中のガスの体積はいずれも標準
状態（０℃、latm）の値である。 Hereinafter, the present invention will be explained in more detail with reference to Examples. Note that all gas volumes in the examples are values under standard conditions (0° C., latm).
実施例 １
容積100mlの円筒状ガラス容器に、CuClを9.90
ｇ（0.1モル）およびFeCl2、4H2Oを4.97ｇ
（0.025モル）採取し、これにＮ−メチルピロリド
ンを51.5ｇ（0.52モル）添加したところ、均一溶
液が得られた。この吸収液を30℃に保ちながら、
CO20％、N280％（容量％）からなる組成のガス
を常圧で連続的に吹き込み、本条件下でのCOの
平衡吸収量を求めた。その結果、本吸収液は１ml
当たり7.0mlのCOを吸収した。比較のために、
CuCl9.9ｇ（0.1モル）を8NHCl水溶液50mlに溶解
させたもの（従来の塩酸酸性第１銅溶液）の同一
条件下におけるCO平衡吸収量を求めたところ、
吸収液１ml当たり4.5mlのCOを吸収するにすぎな
かつた。Example 1 9.90 ml of CuCl was placed in a cylindrical glass container with a volume of 100 ml.
g (0.1 mol) and 4.97 g of FeCl 2 , 4H 2 O
(0.025 mol) was collected, and 51.5 g (0.52 mol) of N-methylpyrrolidone was added thereto to obtain a homogeneous solution. While keeping this absorption liquid at 30℃,
A gas with a composition of 20% CO and 80% N 2 (volume %) was continuously blown in at normal pressure, and the equilibrium absorption amount of CO under these conditions was determined. As a result, this absorption liquid was 1ml.
7.0 ml of CO was absorbed per unit. For comparison,
When 9.9 g (0.1 mol) of CuCl was dissolved in 50 ml of 8NHCl aqueous solution (conventional cuprous hydrochloric acid solution), the equilibrium CO absorption amount was determined under the same conditions.
Only 4.5 ml of CO was absorbed per ml of absorbent.
実施例 ２
実施例１で得られた、平衡量のCOを吸収した
液を、100℃に加熱し50mmHgの減圧状態にしたと
ころ、吸収液１ml当たり7.0mlのCOが回収され
た。Example 2 When the liquid obtained in Example 1 that had absorbed an equilibrium amount of CO was heated to 100°C and reduced in pressure to 50 mmHg, 7.0 ml of CO was recovered per ml of the absorbed liquid.
実施例 ３
実施例１で示したものと同一組成の吸収液を新
たに調整し、これに２％（容量％）の水を添加し
た後、30℃にて24時間放置した。その後、実施例
１と同一条件でCO平衡吸収量を測定した。その
結果、吸収液１ml当たり7.0mlのCOを吸収し、水
を添加しても性能に全く変化がないことが示され
た。Example 3 An absorption liquid having the same composition as that shown in Example 1 was newly prepared, 2% (volume %) of water was added thereto, and the mixture was left at 30° C. for 24 hours. Thereafter, the CO equilibrium absorption amount was measured under the same conditions as in Example 1. The results showed that 7.0 ml of CO was absorbed per ml of absorption liquid, and there was no change in performance even when water was added.
実施例 ４
容積100mlの円筒状ガラス容器にCuClを9.90ｇ
（0.1モル）およびSnCl2を9.48ｇ（0.05モル）採
取し、これにジメチルホルムアミドを47.5ｇ
（0.65モル）添加したのち、100℃で３時間加熱し
たところ、均一溶液が得られた。これを30℃に冷
却したのち、実施例１と同一条件でCOの平衡吸
収量を測定した。その結果、吸収液１ml当たり
5.7mlのCOを吸収した。Example 4 9.90g of CuCl in a cylindrical glass container with a volume of 100ml
(0.1 mol) and 9.48 g (0.05 mol) of SnCl 2 were collected, and 47.5 g of dimethylformamide was added to this.
(0.65 mol) and then heated at 100°C for 3 hours, a homogeneous solution was obtained. After cooling this to 30°C, the equilibrium absorption amount of CO was measured under the same conditions as in Example 1. As a result, per ml of absorption liquid
Absorbed 5.7ml of CO.
実施例 ５
容積100mlの円筒状ガラス容器にCuClを9.90ｇ
（0.1モル）採取し、Ｎ−メチルピロリドンを51.5
ｇ（0.52モル）を添加し、スラリ状の吸収液を得
た。この吸収液に関し、実施例１と同一条件下
で、COの平衡吸収量を求めたところ、吸収液１
ml当たり6.8mlのCOを吸収した。Example 5 9.90g of CuCl in a cylindrical glass container with a volume of 100ml
(0.1 mol) was collected, and 51.5 mol of N-methylpyrrolidone was collected.
g (0.52 mol) was added to obtain a slurry-like absorption liquid. Regarding this absorption liquid, the equilibrium absorption amount of CO was determined under the same conditions as in Example 1.
Absorbed 6.8 ml of CO per ml.
以上、本発明によれば、COを含有する各種の
ガス源からCOを効率良く、かつ安定して分離、
濃縮することができる。すなわち、本発明の吸収
液は水に対して安定で、しかもCO吸収量が非常
に高いため、従来のように水分除去のための前処
理が不要になり、また吸収塔の操作で高圧、低温
を必要とせず、常圧、常温で運転することができ
る。しかもCO吸収負荷を大きくとることができ
るため、溶液循環量が小さくて済み、効率および
経済性の高いCO分離、濃縮プロセスとすること
ができる。 As described above, according to the present invention, CO can be efficiently and stably separated from various gas sources containing CO.
Can be concentrated. In other words, the absorption liquid of the present invention is stable against water and has a very high CO absorption amount, so there is no need for pretreatment to remove water as in the past, and the absorption tower can be operated at high pressure and low temperature. It can be operated at normal pressure and temperature. Furthermore, since the CO absorption load can be increased, the amount of solution circulation can be small, making it possible to achieve a highly efficient and economical CO separation and concentration process.
第１図は、本発明の吸収液を用いた一酸化炭素
分離、濃縮プロセスの一実施例を示すフローシー
トである。
２……吸収塔、３……分離塔、４……熱交換
器、１１……ガス供給ライン。
FIG. 1 is a flow sheet showing an example of a carbon monoxide separation and concentration process using the absorption liquid of the present invention. 2... Absorption tower, 3... Separation tower, 4... Heat exchanger, 11... Gas supply line.
Claims (1)
を含むことを特徴とする一酸化炭素の吸収液。 ２ 特許請求の範囲第１項において、前記吸収液
は、さらに一価の銅以外の遷移金属塩化物を含む
ことを特徴とする一酸化炭素の吸収液。 ３ 特許請求の範囲第１項または第２項におい
て、非プロトン性のアミド系溶媒は、Ｎ−メチル
ピロリドン、テトラメチルウレア、ジメチルホル
ムアミド、ジエチルホルムアミド、およびジメチ
ルアセトアミドからなる群から選ばれた少くとも
一種の化合物であることを特徴とする一酸化炭素
の吸収液。 ４ 特許請求の範囲第２項において、前記遷移金
属塩化物は、三塩化チタン、三塩化バナジウム、
三塩化クロム、二塩化マンガン、二塩化鉄、三塩
化鉄、二塩化銅、塩化亜鉛、塩化ルテニウム、お
よび塩化ランタンからなる群から選ばれた少くと
も一種の化合物であることを特徴とする一酸化炭
素の吸収液。[Scope of Claims] 1. A carbon monoxide absorption liquid characterized by containing cuprous chloride and an aprotic amide solvent. 2. The carbon monoxide absorption liquid according to claim 1, wherein the absorption liquid further contains a transition metal chloride other than monovalent copper. 3. In claim 1 or 2, the aprotic amide solvent is at least one selected from the group consisting of N-methylpyrrolidone, tetramethylurea, dimethylformamide, diethylformamide, and dimethylacetamide. A carbon monoxide absorption liquid characterized by being a type of compound. 4 In claim 2, the transition metal chloride is titanium trichloride, vanadium trichloride,
Monoxide, characterized in that it is at least one compound selected from the group consisting of chromium trichloride, manganese dichloride, iron dichloride, iron trichloride, copper dichloride, zinc chloride, ruthenium chloride, and lanthanum chloride. Carbon absorption liquid.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP2170980A JPS56118721A (en) | 1980-02-25 | 1980-02-25 | Absorption liquid for carbon monoxide |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP2170980A JPS56118721A (en) | 1980-02-25 | 1980-02-25 | Absorption liquid for carbon monoxide |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPS56118721A JPS56118721A (en) | 1981-09-17 |
| JPS6247058B2 true JPS6247058B2 (en) | 1987-10-06 |
Family
ID=12062580
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP2170980A Granted JPS56118721A (en) | 1980-02-25 | 1980-02-25 | Absorption liquid for carbon monoxide |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPS56118721A (en) |
Families Citing this family (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103721528B (en) * | 2013-12-31 | 2017-04-19 | 新疆中泰化学股份有限公司 | Activation absorption apparatus of calcium-carbide-process PVC (polyvinyl chloride) technique |
-
1980
- 1980-02-25 JP JP2170980A patent/JPS56118721A/en active Granted
Also Published As
| Publication number | Publication date |
|---|---|
| JPS56118721A (en) | 1981-09-17 |
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